CN111040798B - Coal-to-liquid low-temperature Fischer-Tropsch reactor - Google Patents
Coal-to-liquid low-temperature Fischer-Tropsch reactor Download PDFInfo
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- CN111040798B CN111040798B CN201911366735.5A CN201911366735A CN111040798B CN 111040798 B CN111040798 B CN 111040798B CN 201911366735 A CN201911366735 A CN 201911366735A CN 111040798 B CN111040798 B CN 111040798B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
- C10G2/344—Apparatus, reactors with moving solid catalysts according to the "fluidised-bed" technique
Abstract
The invention provides a coal-to-liquid low-temperature Fischer-Tropsch reactor with stable temperature and high production efficiency in the reaction process, and the low-temperature Fischer-Tropsch reactor can be used for separating products in the reactor, returning entrained catalyst particles and continuously performing synthetic reaction and product separation, wherein the reactor comprises a loop reaction section, a three-phase separation section, a feed inlet, a discharge outlet and a base; the circulation reaction section comprises a synthesis gas inlet, an inner ring gas distributor, an outer ring gas distributor, a bracket, a circulation cylinder, a boiling water inflow pipe, a water vapor discharge pipe and a baffle plate; the three-phase separation section comprises an overflow weir, a bed layer partition plate, a gas outlet, a liquid outlet, a partition plate, a tangential inlet of a gas-liquid mixed phase, a tangential inlet of a liquid-solid mixed phase, a guide vane, a gas ascending pipe, a liquid ascending pipe and a descending pipe.
Description
Technical Field
The invention belongs to the field of chemical equipment, and particularly relates to a slurry bed Fischer-Tropsch reactor applied to coal-to-liquids, in particular to a low-temperature Fischer-Tropsch reactor for coal-to-liquids.
Background
The world economy is rapidly increased, the demand on oil products such as gasoline, diesel oil and the like is gradually increased, and the indirect liquefaction process for preparing the oil from the coal and the natural gas by Fischer-Tropsch synthesis is more and more emphasized. The Fischer-Tropsch synthetic oil is clean and environment-friendly, has excellent combustion performance, produces high-value chemicals as byproducts, and has high economic benefit.
Introducing H-containing gas into low-temperature slurry bed reactor2And the synthesis gas of CO reacts with the raw material through catalysis at a relatively low temperature to generate heavy hydrocarbon (Fischer-Tropsch wax and the like) products, and the heavy hydrocarbon products are conveyed to a subsequent oil product processing technology.
Slurry bed Fischer-Tropsch reactors are the most common at present, the diffusion effect of synthesis gas in a bed layer in the reaction process is poor, and the synthesis gas is discharged after being unreacted; the main product is liquid phase, carries with catalyst, and also generates gaseous by-products, which results in complex separation process; if the heat released by the reaction cannot be removed in time, the selectivity of the reaction will be lost, and a large amount of gas-phase products are generated.
Chinese patent CN 110180471a discloses a slurry bed reactor for ft synthesis, gas distributor sets up in reactor main part bottom, set up a plurality of groups in the main part and moved heat device and supporting downcomer, it is equipped with liquid-solid separator between the heat device to move, the reactor top is equipped with gas-solid separator, good heat transfer and gas distribution have been realized, but set up the multiunit and moved heat device, a large amount of spaces in the reactor has been occupied, the reaction takes place regionally limitedly, the output is reduced, and the structure is complicated, the construction cost has been increased.
In a slurry bed fischer-tropsch reactor, the heavy hydrocarbons produced are mainly discharged after the catalyst has been separated by a filter. The catalyst which is mixed with heavy hydrocarbon and intercepted by the filter element can be attached to the filter to reduce the flow area, so that the product is accumulated in the bed layer. To avoid this, it is common to blow back the catalyst on the filter after the reaction has proceeded for a period of time to purge it back into the bed. Due to the continuity of the reaction, a catalyst filter layer at the pipe orifice can be quickly formed, the back flushing frequency needs to be improved, and the production efficiency is greatly reduced.
Chinese patent CN 110385089a discloses a slurry bed reactor, wherein, synthesis gas passes through a gas distributor and then uniformly enters a reaction section to contact and react with a catalyst and a solvent, the slurry is forced to back mix in the reaction section after being degassed, a liquid phase product is discharged after passing through a solid-liquid separator, and tail gas is discharged after being deliquored and desolidated, the degassing process is not described in detail, and the slurry is contacted with gas again in the forced back mix process, thereby promoting the circulation reaction, leading the liquid phase product to carry more gas, reducing the effective area of filtration in the solid-liquid separation process, and being unable to realize continuous gas-liquid and liquid-solid separation.
Based on this, in patent CN 108815929a, the fischer-tropsch slurry bed product is output from an external separation device, flows into multiple sets of cyclones to perform gas-liquid separation, the gas phase component is discharged from a gas phase ascending pipe to a gas phase containing zone in the inner cavity of the shell, the liquid-solid phase is discharged from a liquid phase descending pipe to a liquid phase containing zone at the bottom, and is separated by reprecipitation, the catalyst is discharged through an impurity discharge port, the liquid phase product is pumped out by a pump, the whole separation process is performed continuously, but the residual catalyst is sucked into a pump together to cause blocking and abrasion, the whole external separation device has a huge volume, the requirement on the supporting device is high, and the investment cost is not reduced. Therefore, it is highly desirable to develop a low-temperature fischer-tropsch reactor, which can stabilize the temperature during the reaction process, efficiently perform the synthesis reaction, separate three-phase substances, and simultaneously have a simple and compact structure, can realize long-term operation, and reduce the catalyst consumption.
Disclosure of Invention
Based on the aim, the invention provides the slurry bed reactor with stable temperature and high production efficiency in the reaction process, and simultaneously, the product is separated in the reactor, entrained catalyst particles are returned, and the synthesis reaction and the product separation can be continuously carried out.
The technical scheme adopted by the invention is as follows: a coal-to-liquid low-temperature Fischer-Tropsch reactor is used for generating liquid-phase products (Fischer-Tropsch wax and the like), removing heat emitted in the reaction process and separating each phase product from a catalyst, and mainly comprises two parts: the device comprises a circulation reaction section and a three-phase separation section, wherein the circulation reaction section and the three-phase separation section are arranged in the same tank body, and the tank body is arranged on a base;
the whole reactor is perpendicular to the ground, the bottom of the reactor is provided with a discharge hole, the middle of the reactor is provided with a feed inlet, the top of the reactor is provided with a gas outlet, and the side surface of the upper part of the reactor is provided with a liquid outlet. The synthesis gas which participates in the reaction flows upwards from the bottom and sequentially passes through the loop reaction section and the three-phase separation section, and the mixture containing the catalyst in the slurry bed enters the reactor from the middle part and is in full contact reaction with the synthesis gas.
The circulation reaction section comprises a synthetic gas inlet, a gas distributor, a circulation cylinder, a boiling water inflow pipe, a water vapor discharge pipe and a baffle plate; the synthesis gas inlet is arranged on the side surface of the lower part of the tank body and communicated with the gas distributor; the gas distributor is fixed at the bottom of the tank body of the reactor through a support and comprises an inner ring gas distributor and an outer ring gas distributor, the inner ring gas distributor and the outer ring gas distributor are positioned on the same horizontal plane and are communicated with a synthesis gas inlet pipe, the outer ring gas speed is higher, the inner ring gas speed is lower, synthesis gas entering the reactor is sprayed upwards vertically, and due to the fact that the outer ring gas speed is high enough, the gas can push mixed materials to flow upwards, the inner ring gas can increase the air input and improve the reaction speed, and under the difference of the inner ring gas speed and the outer ring gas speed, the materials near the wall surface of the reactor and the materials in the central area form a circular flow.
The circulation cylinder is fixed above the gas distributor and consists of two identical semi-annular cylinders, both ends of each semi-annular cylinder are connected with a boiling water inflow pipe and a water vapor discharge pipe, the boiling water inflow pipe and the water vapor discharge pipe are connected to the outside of the reactor, a plurality of baffle plates are installed inside each semi-annular cylinder in a vertically staggered mode along the circumferential direction, the inside of each semi-annular cylinder is shielded into a vertically zigzag flowing flow channel form, the two semi-annular cylinders divide the section of the tank body of the reactor into an external annular area and an internal circle center area, so that the circulation cylinder can be matched with the gas distributor to form an annular flow channel, and the bed layer moves upwards under the pushing of gas near the wall surface and descends in the central area. The flowing directions of the heat-removing fluid in the two semi-cylinders are opposite.
The heat transfer fluid is introduced into the two semi-annular cylinders, so that heat generated in the reaction process can be removed, and the temperature is prevented from exceeding the reaction interval to generate a large amount of non-target products. The invention combines the heat transfer device and the circulation cylinder, thereby omitting heat exchange equipment such as a heat exchange tube and the like in the conventional reactor, reducing the occupation of the heat exchange tube on the inner space of the reactor, reducing the obstruction to material flow and reducing the existence of dead zones.
The three-phase separation section comprises an overflow weir, a bed layer partition plate, an upper partition plate, a lower partition plate and a gas-liquid-solid three-phase separator, a gas-phase accommodation area is formed between the upper partition plate and the elliptical top of the reactor tank body, a liquid-phase accommodation area is formed between the upper partition plate and the lower partition plate, products flowing out of a single separator are temporarily stored in the gas-phase accommodation area and the liquid-phase accommodation area, and the products are respectively led out from a gas outlet and a liquid outlet of the gas-liquid-solid three-phase separator.
The three-phase separation section and the circulation reaction section are separated by the bed layer partition plate, and the overflow weirs are fixed at two ends of the bed layer partition plate and are about half of the height of the gas-liquid-solid three-phase separator. The gas-liquid-solid three-phase separator comprises six gas-liquid-solid separators, a liquid-solid separation section and a gas-liquid separation section, wherein the six gas-liquid-solid separators are symmetrically distributed between a bed layer partition plate and a lower partition plate, and the liquid-solid separation section comprises a liquid-solid mixed phase tangential inlet, a liquid ascending pipe, a liquid-solid separation cavity and a bottom flow port; the gas-liquid separation section comprises a gas-liquid mixed phase tangential inlet, a gas ascending pipe, a gas-liquid separation cavity and a guide vane; the liquid-solid separation section is characterized in that the uppermost end of the liquid-solid separation section is directly connected with the lowermost end of the gas-liquid separation section, the guide vane is positioned at the connecting part of the gas-liquid separation section and the liquid-solid separation section, the liquid ascending pipe upwards penetrates through the guide vane from the liquid-solid separation cavity and extends into the gas ascending pipe, the liquid ascending pipe penetrates out of the side face of the gas ascending pipe and reaches the liquid phase containing area, the gas ascending pipe upwards extends from the gas-liquid separation cavity to the gas phase containing area, and the underflow port is positioned below the liquid-solid separation cavity and communicated with the downcomer.
The liquid-solid mixed phase tangential inlets face overflow weirs at two ends, the liquid level of a bed layer in the reactor is slightly higher than the overflow weirs, so that a product can flow through a weir body and enter a gas-liquid-solid three-phase separator, a descending pipe of the gas-liquid-solid three-phase separator is inserted into the bed layer, and an outlet of the descending pipe is close to the circulating cylinder. A tangential inlet of a liquid-solid mixed phase of the gas-liquid-solid three-phase separator is fixed on the bed layer partition plate, and a tangential inlet of the gas-liquid mixed phase is fixed below the lower partition plate. The guide vane in the three-phase separator is positioned between the gas-liquid separation cavity and the liquid-solid separation cavity, and the rotating direction of the guide vane is consistent with the mixing phase entering tangentially. The gas ascending pipe and the liquid ascending pipe form a jacket, and the separated gas flows upwards from the annular space of the jacket in the axial direction and enters the gas-phase containing area; the separated liquid flows upwards from the center of the jacket axially and enters the liquid phase holding area.
The working process is as follows: the materials in the slurry bed react with the synthesis gas under the action of the catalyst to form a circulation under the action of the gas distributor and the circulation cylinder, and the circulation cylinder simultaneously plays a role in heat transfer. The product after the reaction flows over the overflow weir and then tangentially enters a gas-liquid-solid three-phase separator, gas is gathered above the liquid level and carries a small amount of liquid drops, the gas-liquid mixture tangentially enters a gas-liquid separation cavity from an inlet, the liquid drops fall along the wall surface under the centrifugal action, and the gas axially moves through a gas riser and enters a gas phase containing area to be led out; the liquid on the wall surface forms rotary motion through the guide vanes, and is mixed with the liquid entering tangentially to the inlet through liquid-solid mixing, solid particles are concentrated in the liquid near the wall surface under the centrifugal motion, and the liquid in the center axially moves to the liquid phase containing area through the liquid ascending pipe and is led out. The liquid carrying a large amount of solids returns to the bed layer from the bottom downcomer, and the separation of gas, liquid and solid phases is realized.
Compared with the existing slurry bed reactor, the invention has the following advantages:
1. a circulation flow is formed inside to fully stir the mixture, so that the contact mixing reaction efficiency is enhanced;
2. the circulation cylinder and the heat exchange equipment are integrally arranged, and simultaneously, good flow guiding and heat transferring effects are achieved, so that the installation space of the reactor is greatly saved, the extra heat exchange equipment such as a heat exchange pipe is omitted, the obstruction to material flow is reduced, and the existence of dead zones is reduced;
3. the gas-liquid-solid three-phase separator realizes the reaction and separation integration in the reactor without external separation equipment;
4. the structure of the gas-liquid-solid three-phase separator is redesigned, the gas-liquid-solid separation section and the gas-liquid separation section are included, the gas-phase liquid removal and liquid-phase solid removal integrated process can be realized, the whole three-phase separator is compact in structure, the internal parts are few, the separator cavity is large enough, the adhesion and blockage of catalyst particles are avoided, back washing is not needed, and the stable long-period operation of the slurry bed reactor can be ensured.
Drawings
FIG. 1 is a schematic view of the apparatus of the present invention;
FIG. 2 is a schematic layout of a three-phase separator in section A-A of the three-phase separation section;
FIG. 3 is a schematic layout of a section of a circulation drum of the circulation reaction section B-B;
FIG. 4 is a three-dimensional perspective view of the internal structure of the recirculation bowl;
FIG. 5 is a schematic view of the flow of heat-removing fluid in the circulation drum;
FIG. 6 is a schematic layout of a gas distributor of section C-C of the loop reaction section;
FIG. 7 is a three-dimensional perspective view of the apparatus;
in the figure, 1-gas riser; 2-a liquid riser; 3-gas-liquid mixing tangential inlet; 4-guide vanes; 5-liquid-solid mixing tangential inlet; 6-a feed inlet; 7-syngas inlet; 8-a base; 9-gas outlet; 10-an upper partition plate; 11-a liquid outlet; 12-a lower baffle; 13-an overflow weir; 14-bed partition board; 15-a downcomer; 16-a discharge outlet; 17-a three-phase separator; 18-a circulation drum; 19-water vapour discharge pipe; 20-boiling water inflow pipe; 21-a baffle plate; 22-inner ring gas distributor; 23-a scaffold; 24-outer ring gas distributor.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
The present invention is described in terms of specific embodiments, and other advantages and benefits of the present invention will become apparent to those skilled in the art from the disclosure herein.
Referring to the drawings, the structures, ratios, sizes, and the like shown in the drawings are only used for matching the disclosure of the present disclosure, so as to be understood and read by those skilled in the art, and are not used to limit the conditions that the present disclosure can be implemented, so that the present disclosure has no technical significance, and any structural modification, ratio relationship change, or size adjustment should still fall within the scope of the disclosure of the present disclosure without affecting the efficacy and the achievable purpose of the present disclosure. Meanwhile, the positional limitation terms used in the present specification are for clarity of description only, and are not intended to limit the scope of the present invention, and changes or modifications of the relative relationship therebetween may be regarded as the scope of the present invention without substantial changes in the technical content.
FIG. 1 is a schematic structural diagram of the device of the present invention, and as shown in the figure, the low-temperature Fischer-Tropsch reactor for coal-to-liquids mainly comprises two parts: the device comprises a circulation reaction section and a three-phase separation section, wherein the circulation reaction section and the three-phase separation section are arranged in the same tank body, and the tank body is arranged on a base 8;
the whole reactor is perpendicular to the ground, the bottom of the reactor is provided with a discharge outlet 16, the middle of the reactor is provided with a feed inlet 6, the top of the reactor is provided with a gas outlet 9, and the side surface of the upper part of the reactor is provided with a liquid outlet 11. The synthesis gas which participates in the reaction enters from a synthesis gas inlet 7 on the side face of the bottom of the reactor and flows upwards, the synthesis gas sequentially passes through a loop reaction section and a three-phase separation section, and a mixture containing a catalyst in a slurry bed enters the reactor from a middle feed inlet 6 and is in full contact reaction with the synthesis gas.
The circulation reaction section comprises a synthetic gas inlet 7, a gas distributor, a circulation cylinder 18, a boiling water inflow pipe 20, a water vapor discharge pipe 19 and a baffle plate 21; as shown in fig. 6, the gas distributor is a schematic layout of a gas distributor with a C-C cross section in a loop reaction section, the gas distributor is fixed at the bottom of a tank body of the reactor through a bracket 23, and comprises an inner ring gas distributor 22 and an outer ring gas distributor 24, the inner ring gas distributor and the outer ring gas distributor are positioned on the same horizontal plane and are both communicated with a feed pipe of a synthesis gas inlet 7, the outer ring gas velocity is higher, the inner ring gas velocity is lower, synthesis gas entering the reactor is ejected vertically upwards, the gas can push mixed materials to flow upwards due to the sufficiently high outer ring gas velocity, the inner ring gas can increase the gas inflow, the reaction velocity is increased, and the material near the wall surface of the reactor and the material in a central area form a loop under the difference of the inner ring gas velocity and the outer ring gas velocity.
As shown in FIG. 3, FIG. 4 and FIG. 5, respectively are a schematic layout diagram of a circulation cylinder with a section B-B of a circulation reaction section, a schematic flow diagram of heat-removing fluid in the circulation cylinder and a three-dimensional perspective view of the internal structure of the circulation cylinder, the circulation cylinder 18 is fixed above the gas distributor and consists of two identical semi-annular cylinders, both ends of each semi-annular cylinder are connected with a boiling water inflow pipe 20 and a water vapor discharge pipe 19, a plurality of baffle plates 21 are arranged inside each semi-annular cylinder in a vertically staggered manner along the circumferential direction, the inside of each semi-annular cylinder is shielded into a flow passage form flowing in a vertically circuitous manner, the two semi-annular cylinders divide the cross section of the tank body of the reactor into an outer annular area and an inner circle center area, so that the circulating cylinder 18 can form a circulating channel by matching with a gas distributor, near the wall surface, the bed layer moves upwards under the push of gas and descends in the center area of the center. The flowing directions of the heat-moving fluids in the two semicircular cylinders are opposite.
The heat transfer fluid is introduced into the two semi-annular cylinders, so that heat generated in the reaction process can be removed, and the temperature is prevented from exceeding the reaction interval to generate a large amount of non-target products. The invention combines the heat transfer device and the circulation cylinder, thereby omitting heat exchange equipment such as a heat exchange tube and the like in the conventional reactor, reducing the occupation of the heat exchange tube on the inner space of the reactor, reducing the obstruction to material flow and reducing the existence of dead zones.
Referring to fig. 1, the three-phase separation section includes an overflow weir 13, a bed partition plate 14, an upper partition plate 10, a lower partition plate 12 and a gas-liquid-solid three-phase separator, a gas-phase accommodation region is formed between the upper partition plate 10 and the elliptical top of the reactor tank, a liquid-phase accommodation region is formed between the upper partition plate and the lower partition plate, products flowing out of a single separator are temporarily stored in the gas-phase accommodation region and the liquid-phase accommodation region, and the products are respectively led out from a gas outlet and a liquid outlet of the gas-liquid-solid three-phase separator.
The three-phase separation section and the circulation reaction section are separated by the bed layer partition plate 14, and the overflow weirs 13 are fixed at two ends of the bed layer partition plate 14 and have the height about half of that of the gas-liquid-solid three-phase separator. FIG. 2 is a schematic layout diagram of a three-phase separator with a section A-A of a three-phase separation section, wherein six gas-liquid-solid three-phase separators are symmetrically distributed between a bed layer partition plate 14 and a lower partition plate 12 and comprise a liquid-solid separation section and a gas-liquid separation section, and the liquid-solid separation section comprises a liquid-solid mixed phase tangential inlet 5, a liquid ascending pipe 2, a liquid-solid separation cavity and a bottom flow port; the gas-liquid separation section comprises a gas-liquid mixed phase tangential inlet 3, a gas ascending pipe 1, a gas-liquid separation cavity and a guide vane 4; the uppermost end of the liquid-solid separation section is directly connected with the lowermost end of the gas-liquid separation section, the guide vane 4 is positioned at the connecting part of the gas-liquid separation section and the liquid-solid separation section, the liquid ascending pipe 2 upwards penetrates through the guide vane 4 from the liquid-solid separation cavity and extends into the gas ascending pipe 1, the liquid ascending pipe 1 penetrates out of the side face of the gas ascending pipe 1 to the liquid phase containing area, the gas ascending pipe 1 upwards extends into the gas phase containing area from the gas-liquid separation cavity, and the underflow port is positioned below the liquid-solid separation cavity and is communicated with the downcomer 15.
The liquid-solid mixed phase tangential inlets 5 face overflow weirs 13 at two ends, the liquid level of the bed layer in the reactor is slightly higher than the overflow weirs 13, so that a product can flow through the weir body and enter the gas-liquid-solid three-phase separator, a downcomer 15 of the gas-liquid-solid three-phase separator is inserted into the bed layer, and the outlet of the downcomer is close to a circulation cylinder 18. A liquid-solid mixing tangential inlet 5 of the gas-liquid-solid three-phase separator is fixed on a bed layer partition plate 14, and a gas-liquid mixing tangential inlet 3 is fixed below a lower partition plate 12. The guide vane 4 in the three-phase separator is positioned between the gas-liquid separation cavity and the liquid-solid separation cavity, and the rotating direction of the guide vane is consistent with the mixing phase entering tangentially. The gas ascending pipe 1 and the liquid ascending pipe 2 form a jacket, and the separated gas flows upwards from the annular space of the jacket in the axial direction and enters a gas phase accommodating area; the separated liquid flows upwards from the center of the jacket axially and enters the liquid phase holding area.
Fig. 7 is a three-dimensional schematic view of the device, and the working process of the device of the invention is explained in conjunction with fig. 1 and 7 as follows: the materials in the slurry bed react with the synthesis gas under the action of the catalyst to form a circulation under the action of the gas distributor and the circulation cylinder, and the circulation cylinder simultaneously plays a role in heat transfer. The product after the reaction flows over the overflow weir and then tangentially enters a gas-liquid-solid three-phase separator, gas is gathered above the liquid level and carries a small amount of liquid drops, the gas-liquid mixture tangentially enters a gas-liquid separation cavity from an inlet, the liquid drops fall along the wall surface under the centrifugal action, and the gas axially moves through a gas riser and enters a gas phase containing area to be led out; the liquid on the wall surface forms rotary motion through the guide vanes, and is mixed with the liquid entering tangentially to the inlet through liquid-solid mixing, solid particles are concentrated in the liquid near the wall surface under the centrifugal motion, and the liquid in the center axially moves to the liquid phase containing area through the liquid ascending pipe and is led out. The liquid carrying a large amount of solids returns to the bed layer from the bottom downcomer, and the separation of gas, liquid and solid phases is realized.
The invention has the following advantages: a circulation flow is formed inside to fully stir the mixture, so that the contact mixing reaction efficiency is enhanced; the circulation cylinder and the heat exchange equipment are integrally arranged, and simultaneously, good flow guiding and heat transferring effects are achieved, so that the installation space of the reactor is greatly saved, the extra heat exchange equipment such as a heat exchange pipe is omitted, the obstruction to material flow is reduced, and the existence of dead zones is reduced; the gas-liquid-solid three-phase separator realizes the reaction and separation integration in the reactor without external separation equipment; the gas-liquid-solid three-phase separator comprises a liquid-solid separation section and a gas-liquid separation section, and can realize the integrated process of gas-phase liquid removal and liquid-phase solid removal.
Although the embodiments of the present invention have been described with reference to the accompanying drawings, it is not intended to limit the scope of the invention, and it should be understood by those skilled in the art that various modifications and changes in equivalent structure or equivalent flow, or direct or indirect application to other related fields without creative efforts based on the technical solutions of the present invention may be made within the scope of the present invention.
Claims (8)
1. A coal-to-liquid low-temperature Fischer-Tropsch reactor is characterized by comprising a loop reaction section and a three-phase separation section, wherein the loop reaction section and the three-phase separation section are arranged in the same tank body; the bottom of the reactor is provided with a discharge port, the middle part of the reactor is provided with a feed inlet, the top of the reactor is provided with a gas outlet, and the side surface of the upper part of the reactor is provided with a liquid outlet;
the circulation reaction section comprises a synthetic gas inlet, a gas distributor, a circulation cylinder, a boiling water inflow pipe, a water vapor discharge pipe and a baffle plate; the synthesis gas inlet is arranged on the side surface of the lower part of the tank body and communicated with the gas distributor; the circulating cylinder is fixed above the gas distributor;
the three-phase separation section comprises an overflow weir, a bed layer partition plate, an upper partition plate, a lower partition plate and a plurality of gas-liquid-solid three-phase separators, wherein a gas phase containing area is formed between the upper partition plate and the elliptical top of the reactor tank body, a liquid phase containing area is formed between the upper partition plate and the lower partition plate, the bed layer partition plate separates the three-phase separation section from the circulation reaction section, the overflow weir is fixed at two ends of the bed layer partition plate, the plurality of gas-liquid-solid three-phase separators are symmetrically distributed between the bed layer partition plate and the lower partition plate and comprise a liquid-solid separation section and a gas-liquid separation section, and the liquid-solid separation section comprises a liquid-solid mixed phase tangential inlet, a liquid ascending pipe, a liquid-solid separation cavity and a bottom flow port; the gas-liquid separation section comprises a gas-liquid mixed phase tangential inlet, a gas ascending pipe, a gas-liquid separation cavity and a guide vane; the uppermost end of the liquid-solid separation section is directly connected with the lowermost end of the gas-liquid separation section, the guide vane is positioned at the connecting part of the gas-liquid separation section and the liquid-solid separation section, the liquid ascending pipe upwards penetrates through the guide vane from the liquid-solid separation cavity to extend into the gas ascending pipe and penetrates out of the side surface of the gas ascending pipe to the liquid phase containing area, the gas ascending pipe upwards extends from the gas-liquid separation cavity to the gas phase containing area, the underflow port is positioned below the liquid-solid separation cavity and is communicated with the descending pipe, the tangential inlet of a liquid-solid mixed phase of the gas-liquid-solid three-phase separator is fixed on the bed layer partition plate, and the tangential inlet of the gas-liquid mixed phase;
the circulation cylinder is composed of two identical semi-annular cylinders, both ends of each semi-annular cylinder are connected with a boiling water inflow pipe and a water vapor discharge pipe, a plurality of baffle plates are arranged inside each semi-annular cylinder in a vertically staggered mode along the circumferential direction, and the two semi-annular cylinders divide the section of the reactor body into an outer annular area and an inner circle center area.
2. The reactor of claim 1, further characterized in that the gas distributor is fixed at the bottom of the tank body of the reactor through a bracket and comprises an inner ring gas distributor and an outer ring gas distributor, wherein the inner ring gas distributor and the outer ring gas distributor are positioned at the same horizontal plane and are communicated with the synthesis gas inlet pipe.
3. The reactor of claim 1, wherein the tank of the reactor is mounted on a base, and the reactor is generally vertical to the ground.
4. The reactor of claim 1, further characterized in that the weir has a height that is half of the height of the gas-liquid-solid three phase separator.
5. Reactor according to claim 1, further characterized in that the number of gas-liquid-solid three-phase separators is chosen to be an even number.
6. The reactor of claim 1 further characterized in that the vane swirl direction is coincident with the mixing tangent to the inlet swirl direction.
7. The reactor of claim 1, further characterized in that the downcomer of the gas-liquid-solid three phase separator is inserted into the bed with the outlet near the ring flow cartridge.
8. The utility model provides a circulation section of thick bamboo of coal system oil low temperature Fischer-Tropsch reactor which characterized in that, the circulation section of thick bamboo comprises two the same semi-annular section of thick bamboos, and the both ends of every semi-annular section of thick bamboo all are connected with boiling water inflow pipe and vapor discharge pipe, and the inside of semi-annular section of thick bamboo is crisscross from top to bottom along circumference and is installed multichannel baffling board, all shelters from the inside of every semi-annular section of thick bamboo into the runner form that upper and lower circuitous flows, two semi-annular section of thick bamboo divide into two regions of outside annular and inside centre of a circle with the.
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